CN111732981B - Flash evaporation gas decarburization dehydration method and device based on membrane separation - Google Patents
Flash evaporation gas decarburization dehydration method and device based on membrane separation Download PDFInfo
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- CN111732981B CN111732981B CN202010524379.1A CN202010524379A CN111732981B CN 111732981 B CN111732981 B CN 111732981B CN 202010524379 A CN202010524379 A CN 202010524379A CN 111732981 B CN111732981 B CN 111732981B
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10L—FUELS NOT OTHERWISE PROVIDED FOR; NATURAL GAS; SYNTHETIC NATURAL GAS OBTAINED BY PROCESSES NOT COVERED BY SUBCLASSES C10G, C10K; LIQUEFIED PETROLEUM GAS; ADDING MATERIALS TO FUELS OR FIRES TO REDUCE SMOKE OR UNDESIRABLE DEPOSITS OR TO FACILITATE SOOT REMOVAL; FIRELIGHTERS
- C10L3/00—Gaseous fuels; Natural gas; Synthetic natural gas obtained by processes not covered by subclass C10G, C10K; Liquefied petroleum gas
- C10L3/06—Natural gas; Synthetic natural gas obtained by processes not covered by C10G, C10K3/02 or C10K3/04
- C10L3/10—Working-up natural gas or synthetic natural gas
- C10L3/101—Removal of contaminants
- C10L3/106—Removal of contaminants of water
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10L—FUELS NOT OTHERWISE PROVIDED FOR; NATURAL GAS; SYNTHETIC NATURAL GAS OBTAINED BY PROCESSES NOT COVERED BY SUBCLASSES C10G, C10K; LIQUEFIED PETROLEUM GAS; ADDING MATERIALS TO FUELS OR FIRES TO REDUCE SMOKE OR UNDESIRABLE DEPOSITS OR TO FACILITATE SOOT REMOVAL; FIRELIGHTERS
- C10L3/00—Gaseous fuels; Natural gas; Synthetic natural gas obtained by processes not covered by subclass C10G, C10K; Liquefied petroleum gas
- C10L3/06—Natural gas; Synthetic natural gas obtained by processes not covered by C10G, C10K3/02 or C10K3/04
- C10L3/10—Working-up natural gas or synthetic natural gas
- C10L3/101—Removal of contaminants
- C10L3/102—Removal of contaminants of acid contaminants
- C10L3/104—Carbon dioxide
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Abstract
The invention relates to the technical field of natural gas treatment and processing, in particular to a flash steam decarbonization and dehydration method and a flash steam decarbonization and dehydration device based on membrane separation, wherein the flash steam decarbonization and dehydration method based on membrane separation is carried out according to the following steps: the rich liquid enters a flash tank for pressure reduction flash evaporation, the fuel gas separated from the membrane separation assembly is discharged by a membrane separation discharge pipeline, and the device comprises the flash tank, a defoaming tank, a heat energy recoverer, an air cooler, a gas-liquid separator, a fine filter, a heat exchanger, a membrane separation assembly and a heater. The invention can perform one-step decarburization dehydration treatment on the flash evaporation gas of the rich liquid generated in the natural gas decarburization process, can recycle the treated rich liquid, can efficiently and safely use the treated flash evaporation dry gas as fuel gas, solves the problems of high operation cost, high management and maintenance difficulty and difficult utilization of low calorific value of the flash evaporation gas, and has the characteristics of safety, labor saving, simplicity, convenience and high efficiency.
Description
Technical Field
The invention relates to the technical field of natural gas treatment and processing, in particular to a method and a device for decarbonizing and dehydrating flash steam based on membrane separation.
Background
Natural gas is widely applied as a clean energy source, in order to meet the rapidly-increasing demand of natural gas, in recent years, high-carbon-content gas fields are increasingly developed, such as domestic Jilin ChangLin gas fields, Daqing Xushen gas fields, middle-sea oil east gas fields, middle-petrochemical Sonnan gas fields, Tarim Akmoma gas fields and the like, according to the requirement of commodity gas quality export standards, raw gas treatment needs to be decarbonized (desulfurized), and the mainstream process of natural gas decarbonization in domestic and foreign gas fields at present mainly adopts an ethanolamine method to meet the requirement of recycling and absorb CO2The alcohol amine solution (rich solution) needs to be regenerated after pressure reduction and flash evaporation, while part of flash evaporation gas can be generated in the pressure reduction process of the rich solution, and the flash evaporation gas has low pressure (0.8 MPa to 1.4 MPa), high temperature and high CO content2（CO240-70% volume content), and if the barren solution is used for reabsorption, the circulation amount is large, the energy consumption is high, and the effect is poor.
The first method is to return to the feed gas after the pressure is increased by a compressorThe inlet enters a decarburization absorption tower; the second is to discharge the burning through a low-pressure discharge torch system; and the third is blending into fuel gas system. Although the first mode can better solve the problem of the outlet of flash evaporation gas, a compressor needs to be additionally arranged, so that the investment is high, the energy consumption is high, the equipment is more, the management and maintenance difficulty is high, and the operation cost is high (reaching 0.5 yuan/cubic); in the second mode, because the flash evaporation gas has high temperature (65-85 ℃), high carbon content and saturated water content, a large amount of free water can be separated out due to temperature drop in the emptying process, and finally accumulated in a pipeline, so that the pipeline corrosion can be accelerated, the freezing and blocking can be easily caused in winter, the potential safety hazard is large, and the high CO content is high 2The phenomenon of incomplete combustion can exist, and the phenomena of environmental pollution and resource waste can be caused; the third mode is not blended into a fuel gas system by decarburization dehydration treatment, because CO2The content is high, the calorific value of the fuel gas is reduced after mixing, the efficiency of the fuel gas equipment is influenced, the heat load is insufficient, the stable operation of a heating system of a treatment plant is influenced, the flash steam is saturated and contains water, the freezing blockage is very easy to cause, and the whole fuel gas system (including the fuel gas equipment) needs to be selected and used for resisting CO for avoiding corrosion2The material(s) of (2) will result in increased investment.
Disclosure of Invention
The invention provides a flash evaporation gas decarbonization and dehydration method and device based on membrane separation, overcomes the defects of the prior art, and can effectively solve the problems of high investment, high energy consumption, more equipment, freezing blockage, pollution, high management and maintenance difficulty and great potential safety hazard of rich liquid flash evaporation gas decarbonization and dehydration in the natural gas decarbonization process.
One of the technical schemes of the invention is realized by the following measures: a flash evaporation gas decarburization dehydration method based on membrane separation is carried out according to the following method: firstly, enabling rich liquid generated in a natural gas decarbonization procedure to enter a flash tank for decompression flash evaporation, discharging liquid obtained after flash evaporation from a regeneration pipeline, and enabling flash evaporation gas obtained after flash evaporation to enter a defoaming tank for defoaming; secondly, the flash evaporation gas after defoaming enters a tube pass of a heat energy recoverer for heat exchange and cooling, and then enters an air cooler for cooling through a heat energy recovery discharge pipeline; thirdly, the flash evaporation gas cooled in the air cooler enters a gas-liquid separator Carrying out gas-liquid separation; fourthly, discharging liquid separated from the gas-liquid separator through a discharge pipeline of the separator, and feeding gas separated from the gas-liquid separator into a fine filter through a feeding pipeline of the fine filter; fifthly, the gas filtered by the fine filter enters the shell side of a heat energy recoverer to exchange heat with flash steam in a heat energy recovery feeding pipeline after defoaming in the tube side of the heat energy recoverer, and the gas after heat exchange and temperature rise in the heat energy recoverer enters the shell side of a heat exchanger to continue temperature rise; sixthly, the gas heated in the heat exchanger enters a membrane separation assembly from a membrane separation feed pipeline for separation, and the water-containing CO separated from the membrane separation assembly2The tail gas is discharged from the deacidification gas system pipeline, and the fuel gas separated from the membrane separation assembly is discharged from the membrane separation discharge pipeline.
The second technical scheme of the invention is realized by the following measures: a device of a flash gas decarburization dehydration method based on membrane separation comprises a flash tank, a defoaming tank, a heat energy recoverer, an air cooler, a gas-liquid separator, a fine filter, a heat exchanger, a membrane separation assembly and a heater, wherein a liquid inlet pipeline is fixedly communicated with an inlet in the middle of the flash tank, a regeneration pipeline is fixedly communicated with an outlet in the bottom of the flash tank, the defoaming tank is seated on the flash tank, an outlet in the top of the flash tank is fixedly communicated with an inlet in the bottom of the defoaming tank, a heat energy recovery feeding pipeline is fixedly communicated between the outlet in the top of the defoaming tank and the inlet in the middle of the heat energy recoverer, a heat energy recovery discharging pipeline is fixedly communicated between the outlet in the middle of the heat energy recoverer and the inlet in the middle of the air cooler, an air cooler discharging pipeline is fixedly communicated between the outlet in the middle of the air cooler and the inlet in the middle of the, a filter discharge pipeline is fixedly communicated between an outlet of the fine filter and an inlet at the top of the heat energy recoverer, a circulating feed pipeline is fixedly communicated with an inlet at the bottom of the heat exchanger, a circulating discharge pipeline is fixedly communicated with an outlet at the bottom of the heat exchanger, a heat exchanger feed pipeline is fixedly communicated between an outlet at the bottom of the heat exchanger and an inlet at the middle of the heat exchanger, a membrane separation feed pipeline is fixedly communicated between an outlet at the middle of the heat exchanger and an inlet at the middle of the membrane separation assembly, a membrane separation discharge pipeline is fixedly communicated with an outlet at the middle of the membrane separation assembly, a liquid discharge pipeline is fixedly communicated with a liquid discharge pipeline on the membrane separation feed pipeline, an acid gas removal system pipeline is fixedly communicated with an air discharge pipeline on the bottom of the membrane separation assembly, an air discharge pipeline on the membrane separation discharge pipeline is fixedly communicated with an air discharge pipeline on the right side of the liquid discharge pipeline inlet, the inlet at the middle part of the heater is fixedly communicated with a heater feeding pipeline.
The following is further optimization or/and improvement of the second technical scheme of the invention:
the heat energy recoverer and the heat exchanger are both of a pipe shell structure.
The membrane separation module is a hollow fiber membrane.
The right side of the middle part of the flash tank is fixedly provided with a flash liquid level meter, a regeneration control valve is fixedly arranged on the regeneration pipeline, and CO is fixedly arranged on the heat energy recovery feeding pipeline in sequence2The device comprises an analyzer, a flash gas pressure gauge and a flash gas control valve, wherein a separator liquid level meter is fixedly arranged at the lower part of a gas-liquid separator, a separator control valve is fixedly arranged on a separator discharge pipe line, a heating thermometer and a one-way valve are fixedly arranged on a heater discharge pipe line in sequence, and CO is fixedly arranged on a membrane separation discharge pipe line between an outlet in the middle of a membrane separation assembly and an inlet of a first emptying pipeline2The analyzer is characterized in that a membrane separation pressure gauge and a membrane separation control valve are sequentially and fixedly mounted on a membrane separation discharging pipeline on the right side of an emptying pipeline inlet, a circulation control valve is fixedly mounted on a circulation liquid inlet pipeline, a heat exchange temperature gauge and a heat exchange pressure gauge are sequentially and fixedly mounted on a membrane separation feeding pipeline between an outlet in the middle of a heat exchanger and a liquid drainage pipeline inlet, and a liquid drainage control valve is fixedly mounted on a liquid drainage pipeline.
The device also comprises a control cabinet, wherein a first signal input end of the control cabinet is electrically connected with a signal output end of a flash evaporation liquid level meter, a first signal output end of the control cabinet is electrically connected with a signal input end of a regeneration control valve, a second signal input end of the control cabinet is electrically connected with a signal output end of a flash evaporation gas pressure gauge, a second signal output end of the control cabinet is electrically connected with a signal input end of a flash evaporation gas control valve, a third signal input end of the control cabinet is electrically connected with a signal output end of a separator liquid level meter, a third signal output end of the control cabinet is electrically connected with a signal input end of a separator control valve, a fourth signal input end of the control cabinet is electrically connected with a signal output end of a membrane separation control valve, a fifth signal input end of the control cabinet is electrically connected with a signal output end of a heat exchange thermometer, a sixth signal input end of the control cabinet is electrically connected with a signal output end of the heat exchange pressure gauge, a sixth signal output end of the control cabinet is electrically connected with a signal input end of the drainage control valve, a seventh signal input end of the control cabinet is electrically connected with a signal output end of the heating thermometer, and a seventh signal output end of the control cabinet is electrically connected with a signal input end of the heater.
The invention can perform one-step decarburization dehydration treatment on the flash evaporation gas of the rich liquid generated in the natural gas decarburization process, can recycle the treated rich liquid, can efficiently and safely use the treated flash evaporation dry gas as fuel gas, solves the problems of high operation cost, high management and maintenance difficulty and difficult utilization of low calorific value of the flash evaporation gas, and has the characteristics of safety, labor saving, simplicity, convenience and high efficiency.
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FIG. 1 is a schematic process flow diagram of the preferred embodiment of the present invention.
The codes in the figures are respectively: 1 is a flash tank, 2 is a defoaming tank, 3 is a heat energy recoverer, 4 is an air cooler, 5 is a gas-liquid separator, 6 is a fine filter, 7 is a heat exchanger, 8 is a membrane separation assembly, 9 is a liquid inlet pipeline, 10 is a regeneration pipeline, 11 is a heat energy recovery feed pipeline, 12 is a heat energy recovery discharge pipeline, 13 is an air cooler discharge pipeline, 14 is a separator discharge pipeline, 15 is a fine filter feed pipeline, 16 is a filter discharge pipeline, 17 is a circulation feed pipeline, 18 is a circulation discharge pipeline, 19 is a heat exchanger feed pipeline, 20 is a membrane separation feed pipeline, 21 is a membrane separation discharge pipeline, 22 is a liquid discharge pipeline, 23 is a deacidification gas system pipeline, 24 is a first blow-down pipeline, 25 is a second blow-down pipeline, 26 is a blow-down pipeline A control cabinet, 27 is a one-way valve, 28 is CO2The analyzer, 29 is a heater, 30 is a heater discharge line, 31 is a heater feed line, 32 is a flash liquid level meter, 33 is a regeneration control valve, 34 is a flash gas pressure gauge, 35 is a flash gas control valve, 36 is a separator liquid level meter, 37 is a separator control valve, 38 is a heating thermometer, 39 is a membrane separation pressure gauge, 40 is a membrane separation control valve, 41 is a circulation control valve, 42 is a heat exchange thermometer, 43 is a heat exchange pressure gauge, and 44 is a drain control valve.
Detailed Description
The present invention is not limited by the following examples, and specific embodiments may be determined according to the technical solutions and practical situations of the present invention. The various chemical reagents and chemicals mentioned in the present invention are all well known and commonly used in the art, unless otherwise specified.
The invention is further described below with reference to the following examples:
example 1: as shown in the attached figure 1, the flash steam decarbonization and dehydration method based on membrane separation is carried out according to the following method: firstly, enabling rich liquid generated in a natural gas decarbonization procedure to enter a flash tank 1 for decompression flash evaporation, discharging liquid obtained after flash evaporation from a regeneration pipeline 10, and enabling flash evaporation gas obtained after flash evaporation to enter a defoaming tank 2 for defoaming; secondly, the flash evaporation gas after defoaming enters a tube pass of a heat energy recoverer 3 for heat exchange and cooling, and then enters an air cooler 4 for cooling through a heat energy recovery discharge pipeline 12; thirdly, the cooled flash steam in the air cooler 4 enters a gas-liquid separator 5 for gas-liquid separation; fourthly, discharging the liquid separated in the gas-liquid separator 5 through a separator discharge pipeline 14, and feeding the gas separated in the gas-liquid separator 5 into the fine filter 6 through a fine filter feeding pipeline 15; fifthly, the gas filtered by the fine filter 6 enters the shell side of the heat energy recoverer 3 to exchange heat with the flash steam which enters the tube side of the heat energy recoverer 3 in the heat energy recovery feeding pipeline 11 and is defoamed, and the gas which is subjected to heat exchange and temperature rise in the heat energy recoverer 3 enters the shell side of the heat exchanger 7 to continue to rise in temperature; sixthly, the gas heated in the heat exchanger 7 enters the membrane separation component 8 from the membrane separation feed line 20 for separation, and membrane separation is carried out Aqueous CO separated in module 82The tail gas is discharged from an acid gas removal system pipeline 23, and the fuel gas separated from the membrane separation assembly 8 is discharged from a membrane separation discharge pipeline 21.
In the prior art, rich liquid flash gas in a natural gas decarbonization device has high decarbonization and dehydration investment, high energy consumption, more equipment, high treatment and operation cost, high management and maintenance difficulty and great potential safety hazard; according to the characteristics of high temperature, low pressure, saturated water content, high carbon content, foam entrainment and the like of the flash evaporation gas of the rich solution, the fuel gas in a factory needs to be taken from the product gas output from the outside, the pressure of the output gas is usually higher, the output gas can be used as the fuel gas after pressure regulation, and the pressure can not be well utilized. The method and the device for decarbonization and dehydration of flash evaporation gas based on membrane separation achieve efficient energy utilization and realize energy conservation and consumption reduction to the maximum extent by optimizing a heat exchange network and performing energy gradient utilization.
Example 2: as shown in attached figure 1, the device for the flash evaporation gas decarburization dehydration method based on membrane separation comprises a flash evaporation tank 1, a defoaming tank 2, a heat energy recoverer 3, an air cooler 4, a gas-liquid separator 5, a fine filter 6, a heat exchanger 7, a membrane separation assembly 8 and a heater 29, wherein a liquid inlet pipeline 9 is fixedly communicated with an inlet in the middle of the flash evaporation tank 1, a regeneration pipeline 10 is fixedly communicated with an outlet in the bottom of the flash evaporation tank 1, the defoaming tank is seated on the flash evaporation tank 1, a top outlet of the flash evaporation tank 1 is fixedly communicated with an inlet in the bottom of the defoaming tank 2, a heat energy recovery feeding pipeline 11 is fixedly communicated between the top outlet of the defoaming tank 2 and an inlet in the middle of the heat energy recoverer 3, a heat energy recovery discharging pipeline 12 is fixedly communicated between the outlet in the middle of the heat energy recoverer 3 and an inlet in the middle of the, a separator discharge pipeline 14 is fixedly communicated with the bottom of the gas-liquid separator 5, a fine filter feeding pipeline 15 is fixedly communicated between an outlet at the top of the gas-liquid separator 5 and an inlet of the fine filter 6, a filter discharge pipeline 16 is fixedly communicated between an outlet of the fine filter 6 and an inlet at the top of the heat energy recoverer 3, a circulating feeding pipeline 17 is fixedly communicated with an inlet at the bottom of the heat exchanger 7, a circulating discharging pipeline 18 is fixedly communicated with an outlet at the bottom of the heat exchanger 7, a heat exchanger feeding pipeline 19 is fixedly communicated between an outlet at the bottom of the heat energy recoverer 3 and an inlet at the middle of the heat exchanger 7, a membrane separation feeding pipeline 20 is fixedly communicated between an outlet at the middle of the heat exchanger 7 and an inlet at the middle of the membrane separation assembly 8, a membrane separation discharge pipeline 21 is fixedly communicated with an outlet at the middle of the membrane separation assembly 8, a liquid, a first emptying pipeline 24 is fixedly communicated with the membrane separation discharging pipeline 21, a second emptying pipeline 25 is fixedly communicated between the deacidification system pipeline 23 and the first emptying pipeline 24, a heater discharging pipeline 30 is fixedly communicated between the membrane separation feeding pipeline 20 on the right side of the inlet of the drainage pipeline 22 and the outlet of the middle part of the heater 29, and a heater feeding pipeline 31 is fixedly communicated with the inlet of the middle part of the heater 29.
In the invention, the spare membrane separation modules 8 can be installed, when one set of membrane separation modules 8 is regenerated, the other set of membrane separation modules 8 can be continuously used, and the normal operation of the membrane separation process is ensured. The flash tank 1 and the defoaming tank 2 can be integrated together, the length of the defoaming tank 2 can be 0.5m to 1.0m, the nominal diameter of the defoaming tank 2 is usually 5 times to 8 times of the diameter of a pipeline, the nominal diameter is not less than 200mm, and CO resistance is arranged in the defoaming tank 22Corroded random or structured packing. The fine filter 6 and the gas-liquid separator 5 can be integrated, the fine filter 6 can be a filter element made of glass fiber and microfiber, and the fine filter 6 can filter liquid drops with the precision of 0.1-0.5 μm. The heater 29 can be an electric heater or heat conducting oil or steam as a heat source. According to the invention, the flow meter, the valve and the skid-mounted base can be installed as required to more safely and effectively decarbonize and dewater the flash evaporation gas of the rich solution.
Example 3: as shown in fig. 1, the heat energy recoverer 3 and the heat exchanger 7 are both tube-shell structures as optimization of the above embodiment. The heat exchanger 7 can use heat conducting oil or steam as a heat source. The temperature of the flash evaporation gas of the rich solution is between 65 and 85 ℃, when the temperature of the flash evaporation gas is higher and reaches between 75 and 85 ℃, the temperature of the gas output from the heat energy recoverer 3 can reach between 70 and 80 ℃, the heat exchanger 7 can not work according to the actual situation, and the gas output from the heat energy recoverer 3 can directly enter the membrane separation assembly 8 for treatment.
Example 4: as shown in fig. 1, the membrane separation module 8 is a hollow fiber membrane as an optimization of the above embodiment. The membrane separation module 8 can be selected from a hollow fiber membrane special for decarburization and having a diameter of 130mm and a length of 1100mm, and when the amount of the treated gas is 25000m3When the pressure is 1.0MPa to 1.2MPa, 10 membranes can be selected to run in parallel, the yield of product gas methane in the membrane separation feed pipeline 20 can reach 90 percent to 95 percent, the water dew point can be minus 5 ℃ to minus 10 ℃, and the gas outlet of the membrane separation component 8 can be provided with a sampling port, a water dew point analyzer or a CO dew point analyzer2The analyzer 28 can increase or decrease the number of membranes in the membrane separation module 8 according to the methane yield and the water dew point requirement, so as to grasp the gas outlet CO of the membrane separation module 82Content, better control the decarburization effect. The membrane separation component 8 can be regenerated by adopting compressed air or nitrogen, the pressure of the compressed air or nitrogen can be 0.4MPa to 1.0MPa, the compressed air or nitrogen can be heated by a heater 29, the regeneration temperature of the membrane separation component 8 can be controlled to be 60 ℃ to 80 ℃, and the gas amount treated by a single group of membranes is 2000m3Calculated as/d, the regeneration gas content of the membrane separation module 8 can be 20m at a temperature of 20 ℃ and a pressure of 101.325kPa3H to 50m3The regeneration period can be 3d to 5d, and when the membrane separation module 8 is undergoing regeneration, the gas in the membrane separation feed line 20 can be vented via vent line 22 to a low pressure flare system for flare.
Example 5: as shown in the attached figure 1, as the optimization of the above embodiment, a flash liquid level meter 32 is fixedly arranged at the right side of the middle part of the flash tank 1, a regeneration control valve 33 is fixedly arranged on the regeneration pipeline 10, and CO is fixedly arranged on the heat energy recovery feeding pipeline 11 in sequence2Analyzer 28, flash gas pressure gauge 34, flash gas control valve 35, and gas-liquid separatorA separator liquid level meter 36 is fixedly arranged at the lower part of the separator 5, a separator control valve 37 is fixedly arranged on the separator discharge pipeline 14, a heating thermometer 38 and a one-way valve 27 are fixedly arranged on the heater discharge pipeline 30 in sequence, and CO is fixedly arranged on the membrane separation discharge pipeline 21 between the middle outlet of the membrane separation component 8 and the inlet of the first emptying pipeline 242The analyzer 28 is characterized in that a membrane separation pressure gauge 39 and a membrane separation control valve 40 are sequentially and fixedly mounted on a membrane separation discharge pipeline 21 on the right side of an inlet of a first emptying pipeline 24, a circulation control valve 41 is fixedly mounted on a circulation liquid inlet pipeline 17, a heat exchange thermometer 42 and a heat exchange pressure gauge 43 are sequentially and fixedly mounted on a membrane separation feed pipeline 20 between an outlet in the middle of a heat exchanger 7 and an inlet of a liquid drainage pipeline 22, and a liquid drainage control valve 44 is fixedly mounted on the liquid drainage pipeline 22.
Example 6: as shown in the attached figure 1, as the optimization of the above embodiment, the system further comprises a control cabinet 26, wherein a first signal input end of the control cabinet 26 is electrically connected with a signal output end of a flash evaporation liquid level meter 32, a first signal output end of the control cabinet 26 is electrically connected with a signal input end of a regeneration control valve 33, a second signal input end of the control cabinet 26 is electrically connected with a signal output end of a flash evaporation gas pressure gauge 34, a second signal output end of the control cabinet 26 is electrically connected with a signal input end of a flash evaporation gas control valve 35, a third signal input end of the control cabinet 26 is electrically connected with a signal output end of a separator liquid level meter 36, a third signal output end of the control cabinet 26 is electrically connected with a signal input end of a separator control valve 37, a fourth signal input end of the control cabinet 26 is electrically connected with a signal output end of a membrane separation pressure gauge 39, a fourth signal output end of the control, a fifth signal output end of the control cabinet 26 is electrically connected with a signal input end of the circulation control valve 41, a sixth signal input end of the control cabinet 26 is electrically connected with a signal output end of the heat exchange pressure gauge 43, a sixth signal output end of the control cabinet 26 is electrically connected with a signal input end of the liquid discharge control valve 44, a seventh signal input end of the control cabinet 26 is electrically connected with a signal output end of the heating thermometer 38, and a seventh signal output end of the control cabinet 26 is electrically connected with a signal input end of the heater 29. The control cabinet 26 can adopt an RTU (remote measurement and control terminal) or a PLC control system, and is communicated with an upper computer through an RS485 interface to realize automatic control.
The invention comprises two parts of flash evaporation gas treatment and membrane regeneration, can determine whether a regeneration flow needs to be set or a detachable type is adopted according to the actual working condition, the flash evaporation tank can be pulled to a factory for regeneration, a skid-mounted structure can be adopted, the flash evaporation tank 1 can be independently installed, the operation is convenient, the maintenance is simple, the membrane separation component 8 can be recycled, the resources are fully saved, the operation is safe, efficient, economical and practical, and if the flash evaporation gas of rich liquid in a treatment plant is 25000m, the treatment plant is supposed to3/d， CO2The content is 60%, if CO is treated by the method2The removal rate is 85 percent (adjustable), and the annual gas recovery rate is about 405 multiplied by 104m3The invention has the advantages of creating about 400 million yuan per year, having good economic benefit, being mainly used for decarbonization and dehydration of rich solution flash steam in the decarbonization process of the high carbon-containing gas field, being also used in occasions similar to the working condition, such as a single well or a gathering and transportation station and the like needing decarbonization and dehydration, and having very wide application prospect.
In conclusion, the invention can perform one-step decarburization dehydration treatment on the flash evaporation gas of the rich solution generated in the natural gas decarburization process, can recycle the treated rich solution, can efficiently and safely use the treated flash evaporation dry gas as fuel gas, solves the problems of high operation cost, high management and maintenance difficulty and difficult utilization of low calorific value of the flash evaporation gas treatment, and has the characteristics of safety, labor saving, simplicity, convenience and high efficiency.
The technical characteristics form an embodiment of the invention, which has strong adaptability and implementation effect, and unnecessary technical characteristics can be increased or decreased according to actual needs to meet the requirements of different situations.
Claims (6)
1. A flash evaporation gas decarburization dehydration method based on membrane separation is characterized by comprising the following steps: firstly, enabling rich liquid generated in a natural gas decarbonization procedure to enter a flash tank for decompression flash evaporation, discharging liquid obtained after flash evaporation from a regeneration pipeline, and enabling flash evaporation gas obtained after flash evaporation to enter a defoaming tank for defoaming; secondly, the flash evaporation gas after defoaming enters a tube pass of a heat energy recoverer for heat exchange and cooling, and then enters an air cooler for cooling through a heat energy recovery discharge pipeline; thirdly, cooling in an air coolerThe cooled flash evaporation gas enters a gas-liquid separator for gas-liquid separation; fourthly, discharging liquid separated from the gas-liquid separator through a discharge pipeline of the separator, and feeding gas separated from the gas-liquid separator into a fine filter through a feeding pipeline of the fine filter; fifthly, the gas filtered by the fine filter enters the shell side of a heat energy recoverer to exchange heat with flash steam in a heat energy recovery feeding pipeline after defoaming in the tube side of the heat energy recoverer, and the gas after heat exchange and temperature rise in the heat energy recoverer enters the shell side of a heat exchanger to continue temperature rise; sixthly, the gas heated in the heat exchanger enters a membrane separation assembly from a membrane separation feed pipeline for separation, and the water-containing CO separated from the membrane separation assembly 2The tail gas is discharged from the deacidification gas system pipeline, and the fuel gas separated from the membrane separation assembly is discharged from the membrane separation discharge pipeline.
2. The device for implementing the decarbonization and dehydration method of flash gas based on membrane separation according to claim 1 is characterized by comprising a flash tank, a defoaming tank, a heat energy recoverer, an air cooler, a gas-liquid separator, a fine filter, a heat exchanger, a membrane separation assembly and a heater, wherein a liquid inlet pipeline is fixedly communicated with an inlet in the middle of the flash tank, a regeneration pipeline is fixedly communicated with an outlet in the bottom of the flash tank, the defoaming tank is seated on the flash tank, an outlet in the top of the flash tank is fixedly communicated with an inlet in the bottom of the defoaming tank, a heat energy recovery feeding pipeline is fixedly communicated between the outlet in the top of the defoaming tank and an inlet in the middle of the heat energy recoverer, a heat energy recovery discharging pipeline is fixedly communicated between an outlet in the middle of the heat energy recoverer and an inlet in the middle of the air cooler, an air cooler discharging pipeline is fixedly communicated, a fine filter feeding pipeline is fixedly communicated between the top outlet of the gas-liquid separator and the inlet of the fine filter, a filter discharging pipeline is fixedly communicated between the outlet of the fine filter and the inlet of the top of the heat energy recoverer, a circulating feeding pipeline is fixedly communicated with the inlet of the bottom of the heat exchanger, a circulating discharging pipeline is fixedly communicated with the outlet of the bottom of the heat exchanger, a heat exchanger feeding pipeline is fixedly communicated between the outlet of the bottom of the heat energy recoverer and the inlet of the middle of the heat exchanger, a membrane separation feeding pipeline is fixedly communicated between the outlet of the middle of the heat exchanger and the inlet of the middle of the membrane separation assembly, a membrane separation discharging pipeline is fixedly communicated with the outlet of the middle of the membrane separation assembly, a liquid discharging pipeline is fixedly communicated with the membrane separation feeding pipeline, an acid gas removing system pipeline is fixedly communicated with the membrane separation discharging pipeline, a first emptying pipeline is fixedly communicated with the membrane, a heater discharge pipeline is fixedly communicated between the membrane separation feed pipeline on the right side of the liquid discharge pipeline inlet and the outlet in the middle of the heater, and a heater feed pipeline is fixedly communicated with the inlet in the middle of the heater.
3. The apparatus of claim 2, wherein the thermal energy recuperator and the heat exchanger are of a shell and tube construction.
4. The apparatus of claim 2 or 3, wherein the membrane separation module is a hollow fiber membrane.
5. The device according to claim 2 or 3, wherein a flash liquid level meter is fixedly arranged at the right side of the middle part of the flash tank, a regeneration control valve is fixedly arranged on the regeneration pipeline, and CO is fixedly arranged on the heat energy recovery feeding pipeline in sequence2The device comprises an analyzer, a flash gas pressure gauge and a flash gas control valve, wherein a separator liquid level meter is fixedly arranged at the lower part of a gas-liquid separator, a separator control valve is fixedly arranged on a separator discharge pipe line, a heating thermometer and a one-way valve are fixedly arranged on a heater discharge pipe line in sequence, and CO is fixedly arranged on a membrane separation discharge pipe line between an outlet in the middle of a membrane separation assembly and an inlet of a first emptying pipeline2The analyzer is characterized in that a membrane separation pressure gauge and a membrane separation control valve are sequentially and fixedly mounted on a membrane separation discharging pipeline on the right side of an emptying pipeline inlet, a circulation control valve is fixedly mounted on a circulation liquid inlet pipeline, a heat exchange temperature gauge and a heat exchange pressure gauge are sequentially and fixedly mounted on a membrane separation feeding pipeline between an outlet in the middle of a heat exchanger and a liquid drainage pipeline inlet, and a liquid drainage control valve is fixedly mounted on a liquid drainage pipeline.
6. The apparatus of claim 5, further comprising a control cabinet, wherein the first signal input of the control cabinet is electrically connected to the signal output of the flash level gauge, the first signal output of the control cabinet is electrically connected to the signal input of the regeneration control valve, the second signal input of the control cabinet is electrically connected to the signal output of the flash gas pressure gauge, the second signal output of the control cabinet is electrically connected to the signal input of the flash gas control valve, the third signal input of the control cabinet is electrically connected to the signal output of the separator level gauge, the third signal output of the control cabinet is electrically connected to the signal input of the separator control valve, the fourth signal input of the control cabinet is electrically connected to the signal output of the membrane separation pressure gauge, the fourth signal output of the control cabinet is electrically connected to the signal input of the membrane separation control valve, the fifth signal input of the control cabinet is electrically connected to, the fifth signal output end of the control cabinet is electrically connected with the signal input end of the circulation control valve, the sixth signal input end of the control cabinet is electrically connected with the signal output end of the heat exchange pressure gauge, the sixth signal output end of the control cabinet is electrically connected with the signal input end of the drainage control valve, the seventh signal input end of the control cabinet is electrically connected with the signal output end of the heating thermometer, and the seventh signal output end of the control cabinet is electrically connected with the signal input end of the heater.
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